RU2317285C2 - Method of separating linear alpha-olefins from saturated hydrocarbons - Google Patents

Abstract

FIELD: petrochemical processes.

SUBSTANCE: starting material, obtained, in particular, in Fischer-Tropsch process, contains linear α-olefins, saturated hydrocarbons, internal olefins, branched olefins, and alcohols. Method comprises (a) bringing starting material into contact with linear polyaromatic compound to form reaction mixture containing linear polyaromatic compound-olefin adducts, unreacted olefins, unreacted polyaromatic compound, and alcohol; (b) separating linear polyaromatic compound-olefin adducts from saturated hydrocarbons to form stream of adducts; (c) partially or selectively dissociating stream of adducts under conditions effective to increase percentage of polyaromatic compound reacted with linear α-olefins to form stream containing linear polyaromatic compound-olefin adducts, dissociated olefins, and unreacted and dissociated linear polyaromatic compound; (d) separating linear polyaromatic compound-olefin adducts from dissociated olefins; (e) dissociating separated linear polyaromatic compound-olefin adducts to form linear polyaromatic compound and olefin product enriched with α-olefin; (f) separating α-olefin-rich olefin product from polyaromatic compound, wherein separated product is enriched with linear α-olefins as compared to other olefins in starting material.

EFFECT: increased concentration of linear α-olefins.

15 cl, 1 dwg, 2 tbl, 2 ex

Description

FIELD OF THE INVENTION

This invention relates to a method for separating linear alpha olefins from saturated hydrocarbons.

State of the art

Many industrial processes produce olefin / saturated hydrocarbon streams, which are mixtures of olefins, saturated hydrocarbons and oxygenates. Olefins are often used in the manufacture of polymers, such as polyethylene, as drilling fluid additives or as intermediates for the production of oil additives and detergents. In some industrial processes, olefin streams are produced by oligomerizing ethylene over an alpha olefin catalyst to produce a mixture of alpha olefins and internal olefins having a wide range of carbon atoms. However, these streams are based on the use of ethylene as a feedstock, which significantly increases the cost of olefin production. On the other hand, the Fischer-Tropsch (FT) process begins with the use of an inexpensive feedstock, namely synthesis gas, usually obtained from natural gas, coal, coke and other carbon compounds for the production of oligomers, including olefins, aromatic compounds, saturated hydrocarbons and oxygenates.

However, the Fischer-Tropsch (FT) method is not very selective with respect to the production of olefins. Although reaction conditions and catalysts can be selected to produce a stream enriched with the desired species in the FT product stream, most FT streams contain other types of compounds that must be separated from olefins, which (olefins) are purified and then sold in various markets. For example, a typical FT commercial stream will contain a mixture of saturated hydrocarbons, olefins and oxygenates such as organic carboxylic acids, alcohols, ethers, esters, ketones and aldehydes. All of these compounds must be isolated from the crude FT stream before a particular composition can be offered for sale. The separation process is further complicated by the fact that the FT stream contains compounds having a wide spectrum in terms of the number of carbon atoms, as well as a wide variety of olefins, varying in the number of C atoms within C ₂ -C ₂₀₀ , including internal linear olefins, linear alpha olefins , internal branched olefins, branched alpha olefins and cyclic olefins, many of which have similar molecular weights. Separation and isolation of these varieties is challenging. Traditional distillation methods are often insufficient to separate varieties with close boiling points.

Various methods have been proposed for efficiently separating various species in an FT stream with sufficient purity to make a particular composition suitable for its intended use.

It would be desirable to carry out the separation process in the FT stream, in which the activity and durability of the separating agent is not reduced due to the presence of impurities such as oxygenates in the stream; which remains active in a wide region of the average number of carbon atoms, in the range of C ₅ -C ₂₀ and in which, in the FT stream, linear alpha-olefins, branched alpha-olefins and paraffins are distinguished.

US Pat. No. 4,946,560 describes a method for separating internal olefins from alpha-olefins by carrying out the Diels-Alder reaction by contacting the feedstock with an adduct-forming compound such as anthracene to form an olefin adduct (Diels-Alder adduct), separating the adduct from the feedstock, dissociation of the olefin adduct by heating to obtain an alpha-olefin enriched anthracene and olefin composition, and separating the anthracene from the alpha olefin.

US Pat. No. 6,184,431 describes a method for separating alpha olefins and internal olefins from saturated compounds by contacting a feedstock with a linear polyaromatic compound to form a reaction mixture containing linear polyaromatic compound adducts with an olefin and saturated hydrocarbons, separating the adducts from saturated hydrocarbons, followed by dissociation of the adducts a linear polyaromatic compound with an olefin to form linear polyaromatic compounds and an olefin composition.

US Pat. No. 6,271,434 describes a process for separating linear alpha olefins from a crude stream containing saturated hydrocarbons, internal olefins, branched olefins and linear alpha olefins by contacting the feedstock with a linear polyaromatic compound to form a reaction mixture containing linear polyaromatic adducts compounds and olefins, separation of adducts from saturated hydrocarbons and dissociation of adducts with the formation of linear polyaromatic compounds and olefins.

However, it is desirable to develop a method carried out by cost-effective means for further separation of the desired products.

SUMMARY OF THE INVENTION

A method for separating linear alpha-olefins from a composition of a feedstock comprising linear alpha-olefins, saturated hydrocarbons, internal olefins, branched olefins and alcohol, including:

a) contacting the feedstock composition with a linear polyaromatic compound under conditions effective to form a reaction mixture containing adducts of a linear polyaromatic compound and olefins, saturated hydrocarbons, unreacted olefins and alcohols, and unreacted polyaromatic compounds;

b) separating the linear polyaromatic compound and olefin adducts from saturated hydrocarbons, unreacted olefins and alcohol in the reaction mixture to form a hydrocarbon stream containing saturated hydrocarbons, unreacted olefins and alcohols, and an adduct stream comprising adducts of the linear polyaromatic compound and olefin and non-linear reactants compound;

c) re-establishing equilibrium in the adduct stream by partial and selective dissociation of the linear polyaromatic compound and olefin adducts under conditions effective to increase the percentage of the polyaromatic compound reacted with the linear alpha olefins compared to all other olefins reacted with the polyaromatic compound in the stream thus obtaining a stream in a state of re-established equilibrium containing adducts of a linear polyaromatic compound Ia-olefin, dissociated olefins, and unreacted and dissociated linear polyaromatic compound;

d) separating the linear polyaromatic compound and olefin adducts from the dissociated olefins in a balanced stream to form an olefin stream containing dissociated olefins and a linear alpha olefin adduct stream containing linear polyaromatic compound and olefin adducts and a linear polyaromatic compound;

e) dissociation of linear polyaromatic compound and olefin adducts in a linear alpha olefin adduct stream to form linear polyaromatic compounds and an alpha olefin enriched olefin product; and

f) separating the alpha olefin enriched olefin product from the polyaromatic compound,

whereby the alpha olefin enriched olefin product is enriched in olefin concentration compared to the olefin concentration in the feed and enriched in linear alpha olefin concentration compared to other olefins in the feed.

In addition, a method for separating linear alpha-olefins from a Fischer-Tropsch feedstock having an average number of carbon atoms in the range of 6 to 16 and having a predominant portion of various olefins within the specified range is provided, wherein said feedstock contains linear alpha olefins, olefins, non-linear alpha olefins, saturated hydrocarbons and alcohols, including:

a) contacting said feedstock with a linear polyaromatic compound comprising anthracene or benzanthracene under conditions effective to form a reaction mixture comprising adducts of a linear polyaromatic compound and an olefin, unreacted olefins, alcohols, saturated hydrocarbons and unreacted polyaromatic compound;

b) separating the linear polyaromatic compound and olefin adducts from saturated hydrocarbons, unreacted olefins and alcohol in the reaction mixture to form a hydrocarbon stream containing saturated hydrocarbons, unreacted olefins and alcohols, and an adduct stream containing linear polyaromatic adducts of olefinic compounds and non-linear reactions ;

c) re-equilibration of the stream with the adducts by partial and selective dissociation of the linear polyaromatic compound and olefin adducts under conditions effective to increase the percentage of the polyaromatic compound reacted with the linear alpha olefins compared to all other olefins reacting with the polyaromatic compound in flow, thereby obtaining a flow in a state of re-established equilibrium, containing adducts of a linear polyaromatic compound and ol efina, dissociated olefins and unreacted and dissociated linear polyaromatic compound;

d) separating the linear polyaromatic compound and olefin adducts from the dissociated olefins in a balanced stream to form an olefin stream containing dissociated olefins and a linear alpha olefin adduct stream containing linear polyaromatic compound and olefin adducts and a linear polyaromatic compound;

e) dissociation of linear polyaromatic compound and olefin adducts in a linear alpha olefin adduct stream to form linear polyaromatic compounds and an alpha olefin enriched olefin product; and

f) separating the alpha olefin enriched olefin product from the polyaromatic compound,

whereby the alpha olefin enriched olefin product is enriched in olefin concentration compared to the olefin concentration in the feed and enriched in linear alpha olefin concentration compared to other olefins in the feed.

Brief Description of the Drawings

The drawing is a process flow diagram depicting the processes of adduct formation, separation, re-equilibrium, separation, dissociation and separation to obtain a composition of linear alpha olefins.

DETAILED DESCRIPTION OF THE INVENTION

This invention relates to a method for the isolation and recovery of alpha olefins from saturated hydrocarbons and alcohols, in particular to a method for separating and optionally recovering linear alpha olefins from saturated hydrocarbons in an FT process stream.

It has been found that in the method, as described in US Pat. No. 6,271,434, in order to obtain high purity alpha olefins, the method consisting in the ADCADC-D final process should be used, and so on, where A is the adduct formation step, D is the distillation step and C mean cracking or dissociation steps. It was found that using the stage of re-establishing the equilibrium R, it is possible to exclude the cracking stage, which can be very complex. Thus, the simplification of the method boils down to A-D-R-D-C-D finite.

The feed stream for processing typically contains olefins, saturated hydrocarbons and alcohols. The class of saturated hydrocarbons, as used herein, includes at least paraffin. The saturated hydrocarbon class may also include other molecules, such as cycloparaffins.

Olefin means any compound containing at least one carbon-carbon double bond. Olefins can be linear, branched, conjugated, containing multiple double bonds at various places along the chain, substituted, unsubstituted, containing aryl or alicyclic groups, or containing heteroatoms.

Olefins may contain aryl residues along with an aliphatic or cycloaliphatic residue in the same compound, or may consist solely of aliphatic, cycloaliphatic residues or cycloaliphatic and aliphatic residues in the compound. Preferably, the olefin is an aliphatic compound.

Olefin may be branched or linear. Examples of branching include alkyl, aryl or alicyclic branches. The number of unsaturated points along the chain is also not limited. Olefin may be mono-, di-, tri-, etc. unsaturated olefin, optionally conjugated. Olefin may also contain acetylene unsaturation.

An alpha olefin is an olefin whose double bond is located at the α and β carbon atoms. The carbon α-atom is any terminal carbon atom, regardless of how long the chain has as compared to the lengths of other chains in the molecule. The alpha olefin may be linear or branched. Branches or functional groups can be located on carbon atoms with a double bond, on carbon atoms located next to carbon atoms with a double bond or anywhere along the main carbon chain. The alpha olefin may also be a polyene, in which two or more unsaturation points can be located anywhere along the molecule, provided that at least one double bond is in the alpha position.

The internal olefin (s) is an olefin whose double bond is located anywhere along the carbon chain with the exception of any terminal carbon atom. The internal olefin may be linear or branched. The position of the branch or substitution in the internal olefin is not limited. Branches or functional groups can be located on carbon atoms with double bonds, on carbon atoms located next to carbon atoms with a double bond or anywhere along the main carbon chain. Also, the olefin may be substituted by chemically reactive functional groups. Examples of chemically reactive functional groups are carboxyl, aldehyde, keto group, thio group, ether, hydroxyl and amine. The number of functional groups in the molecule is not limited. Functional groups can be located anywhere along the main carbon chain.

The feed can be obtained by industrial methods, such as oligomerization of ethylene, optionally followed by isomerization and disproportionation. Alternatively, the feedstock can be produced by the Fischer-Tropsch process, which usually gives a high proportion of paraffins. In the Fischer-Tropsch process, CO is catalytically hydrogenated to form compositions containing aliphatic molecular chains. Other methods for preparing the feedstock, which may contain mixtures of olefins and paraffins, include dehydrogenation of paraffin as is done in the Pacol ^™ process in UOP and cracking of waxes. The most preferred feedstock is Fischer-Tropsch (FT) feedstock.

FT catalysts and reaction conditions can be tailored to provide a specific mixture of species in the reaction product stream. For example, a particular catalyst and reaction conditions can be selected so as to increase the amount of olefins and reduce the amount of paraffins and oxygenates in the stream. Alternatively, the catalyst and reaction conditions can be selected so as to increase the amount of paraffins and reduce the amount of olefins and oxygenates in the stream.

Typically, reaction conditions will vary depending on the type of equipment used. FT reaction temperatures range from 100 ° C to 500 ° C, gas inlet pressure to the reactor from atmospheric pressure to 1,500 psi. inch and the ratio of H ₂ / CO from 0.5: 1 to 5: 1, preferably from 1.8: 1 to 2.2: 1, and the volumetric hourly gas flow rate in the range from 1 to 10,000 vol./about. / hour. Many configurations of reaction vessels may be used, including with a fluidized (moving) bed, a fixed bed and a suspension bed. The temperature in these layers can be adjusted by specialists in order to optimize the formation of FT products, including hydrocarbons and especially olefins, and a variety of olefins. By way of illustration, without limitation, in the fluidized bed (s), the reaction temperature is usually high, for example, in the range from 280 to 350 ° C, preferably from 310 to 340 ° C. If a fixed-bed reactor (s) are used, the reaction temperature is usually in the range of 200 ° C to 250 ° C, preferably 210 and 240 ° C, and when the reactor (s) with the slurry layer are used, the temperature is usually in range from 190 ° C to 270 ° C.

The catalyst used in the FT method is any of those known in the art, but preferably among the compounds Mo, W, and Group VIII, including iron, cobalt, ruthenium, rhodium, platinum, palladium, iridium, osmium, combinations of the above compounds, combinations with other metals, each in the form of a free metal, or in the form of alloys, or in the form of oxide, or carbide, or another compound, or in the form of a salt. The catalysts may also contain activators that promote catalytic activity, stability or selectivity. Suitable activators include alkali or alkaline earth metals in a free state or in a combined form, in the form of an oxide, hydroxide, salt, or combinations thereof. For example, suitable catalysts are described in US patent No. 6271434 and No. 6184431, the contents of which are incorporated into this description by reference.

Typically, the FT process stream is substantially free of sulfur or nitrogen compounds, which may be harmful to other catalysts that derivatize olefins or catalyze olefin reactions in other oligomerization or polymerization processes. However, regardless of the method used, the FT process is not highly selective for specific varieties and leads to a wide variety of varieties in the composition.

Examples of certain species of compounds found in any FT stream include paraffins having a wide range of molecular weight values, alcohols, acids, ketones and aldehydes, and small amounts of aromatic compounds. However, the linear polyaromatic compound used in the method according to the invention is particularly well adapted for separating olefins from saturated hydrocarbons in the FT stream in the presence of oxygenates, since oxygenates slightly impair the effectiveness of the linear polyaromatic compound.

Although reference is made to the FT stream, it should be understood that any stream obtained by any method containing olefins and saturated hydrocarbons is a suitable starting material for the method according to the invention. Most crude FT process streams contain from 5% to 99% olefins, the remainder are saturated hydrocarbons containing paraffins and cycloparaffins, and optionally other compounds, such as aromatic compounds, optionally containing saturated or unsaturated alkyl branches and oxygenates, based on the weight of all ingredients in the feed stream in the method according to the invention. The preferred amount of olefin present in the FT stream is from 15 wt.% To 70 wt.%. The amount of linear alpha olefin in the FT stream is not limited, but preferably ranges from 15 wt.% To 60 wt.%. The number of other olefins, including branched olefins and internal olefins, both linear and branched, is also not limited, but preferably ranges from 1 wt.% To 55 wt.%, More usually from 5 wt.% To 45 wt.%. The amount of paraffin in most FT streams is from 5 wt.% To 99 wt.%.

In some FT streams, the FT catalyst is adjusted to increase the olefin concentration and decrease the paraffin concentration. In these streams, the amount of paraffin typically ranges from 5 to 65% by weight of the stream. In other FT streams where the FT catalyst is controlled to increase the amount of paraffin, the amount of paraffin in the stream is from 65 wt.% To 99 wt.%. Amounts of other compounds in the FT stream, such as oxygenates and aromatics, comprise most of the remainder of the FT stream and are typically present in amounts ranging from 5 wt.% To 30 wt.%. Minor amounts of other by-products and impurities of less than 5 wt.% May be present in most FT streams. The FT stream, which consists essentially of paraffins, olefins, aromatics, and oxygenates, may include similar minor amounts of other by-products and impurities.

The feed can be treated with an FT stream that has been fractionated and / or purified by conventional distillation, extraction, or other separation methods to remove certain paraffins, high and low molecular weight species and oxygenates from the crude stream. When the separation process is carried out by distillation of the adduct-containing reaction mixture, it is preferable that the feedstock used in the method according to the invention contain an average number of carbon atoms in the range of C ₅ -C ₂₀ and in which the predominant olefin species in the feed are in the range of C ₅ -C ₂₀ inclusive.

The adduct-forming polyaromatic compound effectively separates saturated hydrocarbons and alcohols from olefins when the average number of carbon atoms of the feedstock and the predominant olefin species are within the specified range, inclusive, by the formation of the Diels-Alder adduct. When the average number of carbon atoms of the feedstock exceeds C ₂₀ , the adduct of the polyaromatic compound and olefin boils at a lower temperature than many of the substances in the feed composition of C ₂₀ +, thereby leaving these high boiling varieties in the bottom product of the reaction mixture containing the adduct.

Accordingly, the particular polyaromatic compound and the specific composition of the feedstock should be selected so that the adduct composition of the polyaromatic compound and the olefin in the reaction mixture boils at a higher temperature than the amount of unreacted paraffin species in the feedstock that needs to be separated. Therefore, in this preferred embodiment, the feed stream is a stream that contains an average number of carbon atoms in the range of 5 to 20, and more preferably in the range of 6 to 16, and in which the predominant olefin species are within these ranges, inclusive. Typically, these types of FT streams are processed using one of the methods described above to substantially remove fractions containing ingredients below or above the C ₅ -C _{20 region} .

In the case where it is required to use a feedstock that is outside a region characterized by average carbon atoms of 5 to 20, other separation methods can be used to separate the adduct from the unreacted reaction mixture, including the choice of higher boiling polyaromatic compounds and / or other separation methods, such like liquid / liquid extraction or crystallization. Undoubtedly, these methods can also be used with feedstock having an average number of carbon atoms in the range of 5-20 inclusive.

A linear polyaromatic compound is used in this method to form an adduct with olefins in a feed stream. As used herein, the term “linear polyaromatic compound” refers to a linear polyaromatic compound having at least three fused aromatic rings which may be unsubstituted or substituted and have similar adduct-forming properties in the form of an unsubstituted molecule and mixtures thereof. The linearity property shall extend to all three condensed cycles if a compound with three condensed rings is used, to at least four successively condensed cyclic rings, if a compound with four or more condensed rings is used. A linear polyaromatic compound also refers to mixtures of compounds containing, as one of their components, a linear polyaromatic compound, including, but not limited to, coal tar, anthracene oil and any crude mixture containing fractions separated from naphthalene. The linear polyaromatic compound also includes aromatic molecules bonded together by a bridging group such as a hydrocarbon chain, an ether linkage or a ketone group containing a chain, provided that at least three condensed rings are present in a linear arrangement; as well as molecules containing a heteroatom that does not interfere with the separation of olefins from saturated hydrocarbons.

The linear polyaromatic compound has a preferred selectivity with respect to the formation of adducts with linear alpha olefin compounds, secondly with other olefins and, last but not least, with paraffins, with which this compound is virtually unreactive under any operating parameters, with the exception of the conditions of implementation cracking. A preferred linear polyaromatic compound is one that has a selectivity for linear alpha olefin compounds compared to other olefins greater than 1: 1 mol., Preferably 2: 1 or, much more preferably 4: 1.

Non-limiting examples of a linear polyaromatic compound include anthracene, 2,3-benzanthracene, pentacene, and hexacene. Suitable examples of substituents in substituted linear polyaromatic compounds include, but are not limited to, lower alkyl, for example methyl, ethyl, butyl; halogen, for example chlorine, bromine, fluorine; nitro group; sulfate group; sulfonyloxy group; carboxyl; a lower carboalkoxy group, for example a carbomethoxy, carbethoxy group; an amino group; a mono- and di-lower-alkylamino group, for example methylamino, dimethylamino, methylethylamino; amido group; hydroxy group; cyano group; lower alkoxy group, for example methoxy, ethoxy; a lower alkanoyloxy group, for example an acetoxy group; monocyclic aryls, e.g. phenyl, xylyl, toluyl, benzyl, etc. The specific size of the substituent, their quantity and their position should be selected so that they are relatively inert under the reaction conditions and not so large as to block the formation of the Diels-Alder adduct. Suitable substituted linear polyaromatic compounds may be determined by routine experimentation. Examples of suitable linear polyaromatic compounds include 9,10-dimethylanthracene, 9,10-dichloranthracene, 9-methylanthracene, 9-acetylanthracene, 9- (methylaminomethyl) anthracene, 2-chloranthracene, 2-ethyl-9,10-dimethoxyanthracene, anthrobin and 9 -anthryl trifluoromethyl ketone. Preferred linear polyaromatic compounds are anthracene and 2,3-benzanthracene.

The basis of the method according to the invention is composed of at least six process steps in which (a) a linear polyaromatic compound is reacted with a feedstock containing saturated hydrocarbons and various olefins, including linear alpha olefins, branched olefins and internal olefins, to form an adduct an olefin and a linear polyaromatic compound, (b) the adduct is separated from the reaction mixture, usually by instantaneous evaporation or distillation of unreacted components, including saturated hydrocarbons and alcohols in the upper part and returning the adduct as part of the lower stream, (c) the adduct-containing stream is rebalanced under conditions effective to re-equilibrate the stream with the adducts by partially and selectively dissociating the adducts of the linear polyaromatic olefin compound in conditions effective to increase the content of a polyaromatic compound that has reacted with linear alpha olefins with respect to all other olefins that have reacted with p an oliaromatic compound in a stream, thereby obtaining a rebalanced stream containing linear polyaromatic compound and olefin adducts, dissociated olefins and unreacted and dissociated linear polyaromatic compound, (d) the polyaromatic compound and olefin adducts from step (c) are isolated from the mixture in state (c) rebalance; (e) the adducts of the polyaromatic compound and the olefin isolated in step (d) are dissociated to release olefins and regenerate the linear polyaromatic compound; and (f) alpha olefin enriched olefins are separated from the polyaromatic compound. The olefin stream from step (d) may optionally be recycled to the feedstock to step (a). The unreacted and dissociated polyaromatic compound can be recycled to the feedstock in step (a).

The Diels-Alder adduct formation reaction is carried out using the conventional method and reaction zone. An example of a preferred adduct formation reaction zone is a piston flow reactor used in an upflow mode in which both the linear polyaromatic compound and the feed are mixed and continuously fed to the bottom of the piston flow reactor. The reaction products are continuously removed from the top of the reactor.

Another example of a zone suitable for an adduct formation reaction is a continuous mixing reactor (s) configured as a single unit arranged (s) in parallel or in series, in which the olefin and linear polyaromatic compound are continuously added to the tank ( s) for stirring to form a liquid reaction mixture and the reaction mixture is continuously removed from the mixing tank (s).

For feedstocks with a lower boiling point (lighter feedstocks), a bubble column may be preferred as the adduct formation reaction zone. Alternatively, the reaction may be carried out in a batch reactor.

The adduct formation reaction is usually carried out at a temperature in the range in which the linear polyaromatic compound is in liquid form. Accordingly, preferred temperatures range from 200 ° C, preferably from 220 ° C, most preferably from 240 ° C to 290 ° C, preferably to 280 ° C, and most preferably to 265 ° C. Working pressures are not critical and are set to ensure that none of the olefin streams evaporates. The indicated pressure will depend on the olefin feedstock used. Typical operating pressures can range from 50 psi. inch (4.5 kg / m ² ) up to 200 psi inch (15 kg / m ² ). The reaction can be carried out in a gas phase, in a vacuum or in a liquid phase, or in a mixed gas-liquid phase, depending on the volatility of the feedstock, but usually in a liquid phase.

For the formation of adducts, stoichiometric ratios or an excess of either an olefin or a linear polyaromatic compound can be used. The molar ratio of olefin to linear polyaromatic compound is preferably from 0.1: 1 to 10: 1. Preferably, a molar excess of the linear polyaromatic compound is used to ensure complete and significant recovery of all olefins in the adduct formation zone in step (a). When greater selectivity is desired for the formation of linear alpha-olefin adducts in the adduct formation zone, the molar ratio of linear polyaromatic compounds to olefins can be reduced, for example, preferably closer to a molar ratio of from 0.5: 1 to 1.5: 1. The processing time is sufficient time to form an adduct of the required amount of a linear polyaromatic compound with an olefin. Typical reaction times range from 30 minutes to 4 hours in a batch reactor.

An inert solvent can be used to dissolve the olefins of the feedstock or a linear polyaromatic compound or both of them in the reactor. Preferred solvents are hydrocarbon solvents, which are liquids at reaction temperatures and in which olefins, a linear polyaromatic compound, and adducts of an olefin linear polyaromatic compound are soluble. Illustrative examples of suitable solvents include alkanes such as pentane, isopentane, hexane, heptane, octane, nonane and the like; cycloalkanes such as cyclopentane, cyclohexane and the like; and aromatic compounds such as benzene, toluene, ethylbenzene, diethylbenzene and the like. Preferably, the solvent should be a hydrocarbon having 20 carbon atoms or less. The amount of solvent used can vary over a wide range without adversely affecting the reaction.

However, in one embodiment of the invention, the formation of adducts of the feedstock and especially the formation of adducts of a linear polyaromatic compound and an olefin are carried out in the absence of a solvent in order to improve the reaction rate and to avoid additional equipment and process steps for separating the solvent.

After the adduct of the linear polyaromatic compound and the olefin has been formed, the reaction mixture is fed to a separation vessel effective to separate saturated hydrocarbons from the adduct of the linear polyaromatic compound and the olefin to form a saturated hydrocarbon stream and an olefin stream subjected to adduct formation. Due to the large molecular weight and structural differences between the adduct of the linear polyaromatic compound and the olefin and saturated hydrocarbons in the reaction mixture, traditional separation methods are completely suitable for removing unreacted saturated hydrocarbons. For example, non-adduct compounds can be removed from the top either by fractions by vacuum or by flash evaporation of the reaction mixture to leave the linear polyaromatic compound and olefin adduct and the unreacted linear polyaromatic compound as a liquid in the lower part of the vessel. Non-adduct compounds to be removed include saturated hydrocarbons, aromatics and oxygenates such as alcohols, ketones, acids, along with internal and branched olefins that did not form an adduct with a linear polyaromatic compound.

Alternatively, the adduct of the linear polyaromatic compound and the olefin are separated by cooling the reaction mixture until the adduct crystallizes, followed by filtration or centrifugation to remove unreacted olefin.

In most cases, any unreacted linear polyaromatic compound will separate with the adduct of the linear polyaromatic compound and the olefin in the olefin stream subjected to the formation of adducts. Other ingredients, such as small amounts of unreacted high molecular weight olefins, internal olefins and branched olefins may remain in the adduct stream of the olefin.

The improvement consists in adding a reaction zone to establish a re-equilibrium, which can preferably be created using a second reactor after passing through a distillation step in which alkanes, unreacted olefins and various compounds from the product of the adduct formation are removed. This rebalancing reactor (or rebalancing device) can be a piston flow reactor, a continuous stirred reactor (CSTR), a CSTR series, a batch reactor, a bubble column reactor with a downward flow of liquid, in which the liquid phase is used and temperatures intermediate between the adduct formation zone (adduct formation reactor) and the dissociation zone (adduct cracking reactor). Preferably, the reactor can be operated at a temperature in the range of 280 ° C to 310 ° C. Preferably, the re-equilibration reaction is carried out at a higher temperature than the adduct formation reaction. The residence time in the reactor to establish re-equilibrium should usually be long enough to allow the adduct stream in the reactor to establish re-equilibrium to reach equilibrium, as described below. The residence time in the reactor to establish re-equilibrium will usually be from 30 minutes to 6 hours.

The purpose of this reactor to establish re-equilibrium is to allow adducts, a polyaromatic compound (e.g., anthracene), and olefins to reach a new equilibrium, in which some of the adduct is back-cracked (dissociated) to an olefin and a polyaromatic compound. A significantly larger number of adducts of the internal olefin are subjected to cracking than the α-olefin, effectively providing an increase in the selectivity for α-olefin. In addition, a higher reaction temperature takes advantage of the thermodynamics of adduct formation. The equilibrium constant for internal olefins decreases faster with increasing temperature than the equilibrium constant for α-olefin, thus providing an additional increase in selectivity.

After this re-equilibrium, the dissociated or released olefins are removed using one or more separation steps, such as distillation or crystallization. For example, the released olefins can be removed from the top or as fractions by vacuum or by flash evaporation of the reaction mixture to leave the linear polyaromatic compound and olefin adduct and unreacted or dissociated linear polyaromatic compound in still bottoms.

Adding a reactor to establish re-equilibrium can eliminate one stage of dissociation and generally simplifies plant design compared with a combination of two adduct formation cycles to provide the desired linear alpha olefin composition. As a rule, the content of α-olefin in the product is increased by 3+% (mol.).

The next step in the present process is the dissociation of the adduct of a linear polyaromatic compound and a linear alpha olefin. The dissociation method can be carried out by feeding a stream with linear alpha olefin adducts to a dissociation vessel, where the stream with olefin adducts is heated or pyrolyzed at a temperature effective to dissociate the adduct, usually from 250 ° C to 500 ° C, preferably from 300 ° C up to 350 ° C. Said pyrolysis frees the olefins from a linear polyaromatic compound. Typically, most adducts dissociate. Preferably, the adduct dissociates substantially, i.e., at least 90 mol%, more preferably at least 95 mol%. Residues of the adduct are removed with the polyaromatic compounds during separation, and they can be recycled to the reactor to form the adduct. The linear polyaromatic compound is then separated from the resulting mixture using any conventional methods that can be carried out simultaneously with the pyrolysis operation, such as vacuum distillation or instant distillation of olefins together with any impurities at the pyrolysis temperatures, and removing the linear polyaromatic compound in the form of bottoms from adduct dissociation zones. Other separation methods include filtration and centrifugation.

The linear polyaromatic compound may be recycled back to the adduct formation reaction zone. The separated olefin composition is now enriched in concentration with linear alpha olefins relative to the feed to the adduct formation reaction zone, and the concentration of saturated hydrocarbons and branched olefins in the olefin composition is reduced compared to that in the feed. Similarly, when saturated hydrocarbons are separated from the adduct of the linear polyaromatic compound and the olefin in the separation vessel as a saturated hydrocarbon stream, the saturated hydrocarbon stream is enriched in saturated hydrocarbon concentration in comparison to the concentration of saturated hydrocarbon in the feed to the adduct formation reaction zone. Each of the olefin composition and saturated hydrocarbon stream may be recovered and isolated for use in other applications or as intermediates in other reaction methods.

Referring now to the figure, the feedstock 1 enters the reaction zone of the formation of adduct 2, where the feedstock comes into contact with a linear polyaromatic compound, whereby a reaction mixture 3 containing adducts of a linear polyaromatic compound and olefins, saturated hydrocarbons, unreacted olefins, alcohols and unreacted linear polyaromatic compound. The reaction mixture is separated in a separation zone 4 into a hydrocarbon stream 5 containing saturated hydrocarbons, unreacted olefins and alcohols, and an adduct stream 6 containing adducts of a linear polyaromatic compound and an olefin and an unreacted linear polyaromatic compound. The adduct stream is fed to a re-equilibrium zone 7, where the adduct stream is heated to an equilibrium temperature, whereby a re-equilibrium stream 8 is obtained containing adducts of a linear polyaromatic compound and an olefin, dissociated olefins and an unreacted linear polyaromatic compound and a dissociated linear polyaromatic compound. The equilibrium is established at a temperature effective to increase the proportion of the polyaromatic compound that has reacted with linear alpha olefins with respect to all other olefins that have reacted with the polyaromatic compound in the stream. The re-equilibrium stream is separated in the separation zone 9 into an olefin stream 10 containing dissociated olefins and a linear alpha olefin adduct stream 11 containing adducts of a polyaromatic compound and an olefin and an unreacted and dissociated linear polyaromatic compound. The adducts of the polyaromatic compound and the olefin dissociate (or crack) in the dissociation zone 12 to form linear polyaromatic compounds and the olefin product enriched in linear alpha-olefin, thereby obtaining a dissociated stream 13. The olefin product enriched in alpha-olefin is separated in the separation zone 14 into polyaromatic compound 15 and alpha-olefin-rich olefin product 16.

In order to determine whether, as a result of this method, an increase or decrease in the content of a component occurs, the concentration of this component in the feedstock and in the product stream is considered. If the concentration of the component in the feedstock is higher than its concentration in the product, then this method reduces the content of the component. If the concentration of the component in the product stream is higher than its concentration in the feedstock, then this method enriches for this component. In order to determine whether enrichment or reduction of the content of a set of components occurs in this way, the sum of the concentrations of the components of the set in the feedstock and product stream is considered. If the sum of the concentrations of the components of the kit in the feedstock is higher than the sum of their concentrations in the product, then this method reduces the content of the kit of components. If the sum of the concentrations of the components of the kit in the product stream is higher than the sum of their concentrations in the feedstock, then this method enriches the given set of components.

When the content of a component (set of components) is reduced by this method, the reduction in the percentage of components (set of components) is calculated by subtracting the concentration of the component (the sum of the concentrations of the components of the set) from the concentration of the component (the sum of the concentrations of the components of the set) in the feed, then dividing the indicated difference by the concentration of the component (the sum of the concentrations of the components of the kit) in the feedstock and then multiplying by 100. When the component (kit of components) is enriched by yes method, enrichment in percent for this component (set of components) is calculated by subtracting the concentration of the component (the sum of the concentrations of the components of the kit) in the feedstock from the concentration of the component (the sum of the concentrations of the components of the kit) in the product stream, then dividing the resulting difference by the concentration of the component (the sum of the concentrations of the components set) in the feedstock and then multiplying by 100.

100=87,5%.For example, consider the case where the feedstock contains 40% hexane, while the product stream in this method contains only 5% hexane. Thus, the hexane content is reduced by this method. The percentage reduction of hexane is obtained as ((40-5) / 40)

100 = 87.5%.

100=157,1%. Принимая во внимание только 2-децен, данным способом уменьшают содержание 2-децена. Уменьшение содержания 2-децена в процентах получают равным ((5-2)/5)

100=60%. Рассматривая набор олефинов (т.e. 1-децен и 2-децен), данным способом осуществляют обогащение по набору олефинов. Процентное обогащение по набору олефинов получают ((90+2)-(35+5))/(35+5))

100=130%.For example, consider the case where the feedstock contains 35% 1-decene and 5% 2-decene, while the product stream contains 90% 1-decene and 2% 2-decene. Considering only 1-decene, the content of 1-decene is increased in this method. Percent enrichment at 1-decene is obtained in the form of ((90-35) / 35)

100 = 157.1%. Considering only 2-decene, the content of 2-decene is reduced by this method. The percentage reduction of 2-decene is equal to ((5-2) / 5)

100 = 60%. Considering a set of olefins (i.e., 1-decene and 2-decene), this method enriches a set of olefins. Percent enrichment over a set of olefins is obtained ((90 + 2) - (35 + 5)) / (35 + 5))

100 = 130%.

Another measure of enriching or reducing the content of this method is to enrich or reduce the content of a subgroup of a set of components relative to the set of components. In order to determine whether the enrichment or reduction of the content of a subgroup of a set of components occurs as a result of this method, the sum of the concentrations of the subgroup in the feedstock and in the product stream is considered. If the sum of the concentrations of the subgroup in the feedstock is higher than the sum of the concentrations of the subgroup in the product, then the method reduces the content of the subgroup of the set of components. If the sum of the concentrations of the subgroup in the product stream is higher than the sum of the concentrations of the subgroup in the feedstock, this method enriches the set of components in the subgroup.

100=118,5%. Пусть теперь 2-децен является подгруппой. Содержание подгруппы 2-децена уменьшается относительно набора компонентов, потому что ее концентрация в продукте ниже. Процентное содержание подгруппы 2-децена в продукте составляет 2/(90+2)

100=2,17%. Процентное содержание подгруппы 2-децена в исходном сырье составляет 5/(35+5)

100=12,5%. Таким образом, содержание 2-децена уменьшается с 12,5% до 2,17% в наборе компонентов. Процентное уменьшение содержания 2-децена относительно 1-децена и 2-децена получают ((12,5-2,17)/12,5)

100=816%.You can use two measures to reduce the content or enrichment of a subgroup of a set of components. In case of reduction, the value of the first measure is calculated in a two-stage way. Divide the sum of the concentrations of the subgroup in the feed by the sum of the concentrations of the set of components in the feed and then multiply by 100. This value is called X%. Divide the sum of the concentrations of the subgroup in the product stream by the sum of the concentrations of the set of components in the product stream and then multiply by 100. This value is called Y%. Then they say that the subgroup relative to the set will be reduced from X% to Y%, where Y is less than X. In case of reduction, the size of the second measure is obtained from the first measure by subtracting Y% from X%, then dividing the resulting difference by X% and then multiplying by 100. The foregoing is called the percentage reduction in the content of the subgroup relative to the set of components. In the case of enrichment, the magnitude of the first measure is calculated in a two-stage way. Divide the sum of the concentrations of the subgroup in the feed by the sum of the concentrations of the set of components in the feed and then multiply by 100. This value is called X%. Divide the sum of the concentrations of the subgroup in the product stream by the sum of the concentrations of the set of components in the product stream and then multiply by 100. This value is called Y%. Then they say that the content of the subgroup relative to the set will be increased from X% to Y%, where Y is greater than X. In the case of enrichment, the size of the second measure is obtained from the first measure by subtracting X% from Y%, then dividing the resulting difference by X% and then multiplying by 100. The above is called the percentage enrichment of the subgroup relative to the set of components. For example, consider the case where the feedstock contains 35% 1-decene and 5% 2-decene, while the product stream contains 90% 1-decene and 2% 2-decene. Let 1-decen and 2-decen be a set of components. Let 1-decen be a subgroup. Enrichment is carried out according to the subgroup of 1-decene relative to the set of components, because its concentration in the product is higher. The percentage of the 1-decene subgroup in the set of 1-decene and 2-decene in the product (Y%) is 90 / (90 + 2) = 97.83%. The percentage of the 1-decene subgroup in the feedstock (X%) is 35 / (35 + 5) = 87.5%. Thus, the content of 1-decene increases from 87.5% to 97.83% in the set of components. Percent enrichment at 1-decene relative to 1-decene and 2-decene is equal to ((97.83-87.5) / 87.5)

100 = 118.5%. Now let 2-decen be a subgroup. The content of the 2-decene subgroup is reduced relative to the set of components, because its concentration in the product is lower. The percentage of the 2-decene subgroup in the product is 2 / (90 + 2)

100 = 2.17%. The percentage of the 2-decene subgroup in the feedstock is 5 / (35 + 5)

100 = 12.5%. Thus, the content of 2-decene decreases from 12.5% to 2.17% in the set of components. The percentage reduction in the content of 2-decene relative to 1-decene and 2-decene is obtained ((12.5-2.17) / 12.5)

100 = 816%.

The method according to the invention will increase the total concentration of linear alpha olefins and lower the concentration of saturated hydrocarbons and other olefins, such as branched olefins and internal olefins, compared with their respective concentrations in the feedstock.

In one embodiment, the concentration of all olefins in the saturated hydrocarbon stream is reduced by at least 15%, preferably at least 30%, more preferably at least 50%, by the process of the invention in just one pass to the concentration of all olefins in the feedstock. In another embodiment, the concentration of linear alpha olefins in the saturated hydrocarbon stream is reduced in one pass by at least 30%, more preferably at least 40%, most preferably at least 60% with respect to the concentration linear alpha olefins present in the feed stream.

The amount of excess linear polyaromatic compound present in the adduct formation reaction zone, processing time and temperature will affect the number of internal or branched olefins forming adducts with a linear polyaromatic compound, and therefore a certain amount of internal or branched olefins remains unreacted and transferred to the stream of saturated hydrocarbons. Although the linear polyaromatic compound preferably forms linear alpha-olefin adducts, the presence of a large excess of the polyaromatic compound relative to the amount of linear alpha-olefins present in the feedstock, combined with long residence times, will leave non-formed linear polyaromatic compound adducts to form an adduct with internal and branched olefins, thereby enhancing the reduction of these olefins in the saturated hydrocarbon stream over Alignment with the concentration of olefins in the data stream of the feedstock. In another embodiment, the concentration of internal olefins present in the saturated hydrocarbon stream is reduced by 1-50% compared to the concentration of linear internal olefins present in the feed.

In another embodiment, the concentration of saturated hydrocarbons in the alpha-olefin enriched olefin product is reduced by the method according to the invention in just one pass, at least 80%, preferably at least 90%, more preferably at least , 95% relative to the concentration of saturated hydrocarbon in the feedstock and most preferably 100%.

As before, the percentage decrease or increase in the content of branched olefins and internal olefins in the olefin composition depends on the amount of the linear polyaromatic compound, the temperature, and the residence time of the feedstock in the adduct formation reaction zone. In one embodiment, the concentration of branched olefins in the olefin composition is reduced compared to the concentration of branched olefins in the feed.

In this invention, the concentration of linear alpha olefins in the olefin composition is increased compared to the concentration of linear alpha olefins present in the feed stream. In an embodiment of the invention, the concentration of linear alpha olefins present in the olefin composition is increased by at least 100%, more preferably at least 140%, most preferably at least 155% compared to the concentration linear alpha olefins present in the feed composition. The concentration of linear alpha olefins after the separation step (f) is at least 90%, preferably at least 95%, more preferably at least 96 wt.% Of the total concentration of olefins.

In another embodiment, the concentration of all olefins in the composition of olefins is increased compared to the concentration of all olefins in the feed stream. The degree of olefin enrichment varies inversely with the concentration of all olefins present in the feedstock. In a preferred aspect of this embodiment, the concentration of all olefins in the olefin composition is increased by at least 50%, preferably at least 75%, more preferably at least 90%. The concentration of linear alpha olefin is increased by at least 92%, preferably at least 96 wt.% Of the total concentration of olefins.

Fischer-Tropsch streams contain many difficult to separate components, including saturated hydrocarbons, aromatics, oxygenates, internal olefins, branched olefins and linear alpha olefins. The advantage of the Fischer-Tropsch stream is that it contains a mixture of compounds with both an even and an odd number of carbon atoms, and the method according to the invention provides a stream containing olefin components with an even and odd number of carbon atoms at very close to zero saturated hydrocarbons with high concentrations of linear alpha olefins. The method of the invention may also provide a Fischer-Tropsch olefin composition comprising a mixture of internal olefins and / or branched olefins and linear alpha olefins with low amounts of saturated hydrocarbons.

The method according to the invention advantageously provides a linear alpha olefin stream that is highly concentrated with respect to linear alpha olefins, in which the concentration of linear alpha olefins in the linear alpha olefin composition may be at least 90%, preferably 96% pure linear alpha olefins in the composition of linear alpha olefins.

The flow of the linear alpha olefin composition according to the invention is applicable as a component of drilling fluids, for interaction with elemental sulfur to form sulfonated products, as an agent for ultrahigh pressures in metal processing solutions, as co-monomers in polymerization of polyethylene, as an intermediate in the preparation of poly (alpha-olefins) (PAO) used as a lubricant, as a raw material for chlorination in the production of polychlorinated hydrocarbons in PVC applications, for entering reacting with hydrogen sulfide in the manufacture of primary and secondary mercaptans, as pharmaceutical intermediates and as additives for modifying the properties of rubber, as solvents and as precursors for the production of alcohol plasticizers and detergents of alcohols and surfactants, which can be derivatized to detergent sulphates or alkoxysulphates suitable for laundry liquids and powders, dishwashing powders and liquids, cusco soap, shampoo, liquid hand soap and hard surface cleaners.

The limits and limitations indicated in the present description and claims are the limits and limitations, which are believed to particularly emphasize and clearly express this invention. However, it should be understood that it is understood that other limits and limitations that essentially perform the same function in essentially the same way to obtain the same or essentially the same result are included in the scope of the present invention. The present invention will now be illustrated by the following illustrative embodiments and examples, which are given to illustrate and should not be construed as limiting the scope of this invention.

The examples below are predictions based on the constructed plant model using Aspen10 AspenTech chemical simulation software. Important features of the method of the invention result from the reaction equations described below and the kinetic velocity constants shown in the table below, which were derived from reaction research experiments.

All reactions obey the expression of kinetic velocities :

The units of concentration are mol / liter. Velocity constants are expressed in units of time as reverse hours.

1-olefin 250 ° C 0.51 0,07 280 ° C 1,63 0.72 310 ° C 4.60 6.51 2-methyl-1-olefin 250 ° C 0.11 0.25 280 ° C 0.48 3.38 310 ° C 1.77 37.05 Internal trans olefin 250 ° C 0.11 0.04 280 ° C 0.48 0.57 310 ° C 1.77 6.30 Internal cis olefin 250 ° C 0.11 0.65 280 ° C 0.48 7.81 310 ° C 1.77 76.14

Example 1

The feedstock consisting of C9 / C10 olefins, C9 / C10 alkanes and C7 / C8 alcohols (see Table 1) is reacted with anthracene in an anthracene / olefin molar ratio of 2/1 in a piston flow reactor with a retention time 4.5 hours. The mixture exits the reactor at 260 ° C. Alkanes, unreacted olefins and alcohols are separated from anthracene and adducts at two stages of distillation. The anthracene / adduct stream is then fed sequentially to two continuous stirred tank reactors to crack the adduct. Olefin is selected as a steam product and distilled to remove anthracene. Table 1 compares the composition of the product and the feedstock.

Table 1
No reactor for rebalancing Feedstock Product Composition (wt.%) 1-olefin 37.5 93.35 2-methyl-1-olefin 4,5 2.82 internal trans olefin 3.0 3.82 internal cis olefin 3.0 Trace amounts alkane 47.0 Trace amounts alcohol 5,0 Trace amounts The composition is the main component only olefin (wt.%) 1-olefin 78.12 95.36 2-methyl-1-olefin 9.38 2.82 internal trans olefin 6.25 3.82 internal cis olefin 6.25 Trace amounts Speed, lbs / hour 84000 26247

Example 2

The feedstock consisting of C9 / C10 olefins, C9 / C10 alkanes and C7 / C8 alcohols (see Table 2) is reacted with anthracene in an anthracene / olefin molar ratio of 2/1 in a piston flow reactor with a retention time 4.5 hours. The mixture exits the reactor at 260 ° C. Alkanes, unreacted olefins and alcohols are partially separated from anthracene and adducts using the first of two stages of distillation. After the first distillation step, the product of the bottom of the reactor, enriched in anthracene / adduct, is then fed to the reactor with a piston stream for re-equilibration. The retention time under conditions of re-equilibrium is ~ 0.8 hours. The product exits the reactor for re-equilibration at 290 ° C. Then the specified product is fed to the second stage of distillation to remove all alkanes, most free / unreacted olefins and all alcohol. Then, the anthracene / adduct stream is successively fed to two continuous stirred tank reactors to crack the adduct. Olefin is selected as a steam product and distilled to remove anthracene. Table 2 compares the composition of the product and the feedstock.

table 2
With a rebalancing reactor Feedstock Product Composition (wt.%) 1-olefin 37.5 95.67 2-methyl-1-olefin 4,5 0.89 internal trans olefin 3.0 3.42 internal cis olefin 3.0 Trace amounts alkane 47.0 Trace amounts alcohol 5,0 Trace amounts The composition is the main component only olefin (wt.%) 1-olefin 78.12 95.69 2-methyl-1-olefin 9.38 0.89 internal trans olefin 6.25 3.42 internal cis olefin 6.25 Trace amounts Speed, pound / hour 84000 20562

Claims (15)

1. The method of separation of linear alpha olefins from the composition of the feedstock containing linear alpha olefins, saturated hydrocarbons, internal olefins, branched olefins and alcohol, including: a) contacting the feedstock composition with a linear polyaromatic compound under conditions effective to form a reaction mixture containing adducts of a linear polyaromatic compound and olefins, saturated hydrocarbons, unreacted olefins, alcohols and unreacted polyaromatic compound; b) separating the linear polyaromatic compound adducts and olefins from saturated hydrocarbons, unreacted olefins and alcohol in the reaction mixture to form a hydrocarbon stream containing saturated hydrocarbons, unreacted olefins and alcohols, and an adduct stream containing linear polyaromatic compound adducts and an olefin and unreacted linear reaction ; c) re-establishing the equilibrium (equilibrium state) in the adduct stream by partial and selective dissociation of the adducts of the linear polyaromatic compound and the olefin under conditions effective to increase the percentage of the polyaromatic compound reacted with linear alpha olefins compared to all other olefins that have reacted with polyaromatic compound in the stream, thereby obtaining a stream in a state of re-achieved equilibrium containing linear poly adducts Panchromatic compound-olefin, dissociated olefins, and unreacted and dissociated linear polyaromatic compound; d) separating the linear polyaromatic compound and olefin adducts from the dissociated olefins in an equilibrium stream to form an olefin stream containing dissociated olefins and a linear alpha olefin adduct stream containing linear polyaromatic and olefin adducts and a linear polyaromatic compound; e) dissociation of linear polyaromatic compound and olefin adducts in a linear alpha olefin adduct stream to form linear polyaromatic compounds and an alpha olefin enriched olefin product; and f) separating the alpha olefin enriched olefin product from the polyaromatic compounds, where the olefin product enriched in alpha-olefin is enriched in the concentration of olefins compared to the concentration of olefins in the feedstock and enriched in the concentration of linear alpha-olefins compared to other olefins in the feedstock. 2. The method according to claim 1, in which the processing mode in stage c) is implemented at a higher temperature than the processing mode in stage a). 3. The method according to claim 2, in which, in step c), the adduct stream is rebalanced by heating the adduct stream at a temperature of from about 280 to 310 ° C. 4. The method according to claim 2, in which the feedstock is subjected to contact with a linear polyaromatic compound in stage a) at a temperature of from about 200 to 290 ° C. 5. The method according to claim 2, in which the molar ratio of olefins in the feed to linear polyaromatic compounds is in the range from greater than 0.1: 1 to 10: 1. 6. The method according to claims 1-5, in which the feedstock contains a stream obtained in the Fischer-Tropsch process. 7. The method according to claims 1-5, in which the adduct of the linear polyaromatic compound and the olefin are dissociated by heating the adduct of the linear polyaromatic compound and the olefin at a temperature of from about 250 to 500 ° C. 8. The method according to claim 7, in which the feedstock contains a stream obtained in the Fischer-Tropsch process. 9. A method of separating linear alpha olefins from a feedstock having an average carbon number of 5 to 20 and having a predominant olefin component within the specified range, said feedstock containing olefins and saturated hydrocarbons and alcohols, including: a) contacting the feedstock composition with a linear polyaromatic compound under conditions effective to form a reaction mixture containing adducts of a linear polyaromatic compound and olefins, saturated hydrocarbons, unreacted olefins, alcohols and unreacted polyaromatic compound; b) separating the linear polyaromatic compound adducts and olefins from saturated hydrocarbons, unreacted olefins and alcohol in the reaction mixture to form a hydrocarbon stream containing saturated hydrocarbons, unreacted olefins and alcohols, and an adduct stream containing linear polyaromatic compound adducts and an olefin and unreacted linear reaction ; c) re-establishing the equilibrium (equilibrium state) in the adduct stream by partial and selective dissociation of the adducts of the linear polyaromatic compound and the olefin under conditions effective to increase the percentage of the polyaromatic compound reacted with linear alpha olefins compared to all other olefins that have reacted with polyaromatic compound in the stream, thereby obtaining a stream in a state of re-achieved equilibrium containing linear poly adducts Panchromatic compound-olefin, dissociated olefins, and unreacted and dissociated linear polyaromatic compound; d) separating the linear polyaromatic compound and olefin adducts from the dissociated olefins in an equilibrium stream to form an olefin stream containing dissociated olefins and a linear alpha olefin adduct stream containing linear polyaromatic and olefin adducts and a linear polyaromatic compound; e) dissociation of linear polyaromatic compound and olefin adducts in a linear alpha olefin adduct stream to form linear polyaromatic compounds and an alpha olefin enriched olefin product; and f) separating the alpha olefin enriched olefin product from the polyaromatic compounds, where the olefin product enriched in alpha olefin is enriched in the concentration of olefins compared to the concentration of olefins in the feedstock and enriched in the concentration of linear alpha olefins in comparison with other olefins in the feedstock. 10. The method according to claim 9, in which the feedstock contains a stream obtained in the Fischer-Tropsch process. 11. The method according to claim 9, in which the processing mode in stage c) is implemented at a higher temperature than the processing mode in stage a). 12. The method according to claim 11, in which, in step c), the adduct stream is rebalanced by heating the adduct stream at a temperature of about 280 to 310 ° C. 13. A method for separating linear alpha-olefins from feedstock from the Fischer-Tropsch process having an average number of carbon atoms of 6 to 16 and having a predominant olefin component within the specified range, said feedstock containing linear alpha-olefins, olefins other than linear alpha olefins, saturated hydrocarbons and alcohols, including: a) contacting said feedstock with a linear polyaromatic compound containing anthracene or benzanthracene under conditions effective to form a reaction mixture containing adducts of a linear polyaromatic compound and olefins, unreacted olefins, alcohols, saturated hydrocarbons and unreacted polyaromatic compound; b) separating the linear polyaromatic compound adducts and olefins from saturated hydrocarbons, unreacted olefins and alcohol in the reaction mixture to form a hydrocarbon stream containing saturated hydrocarbons, unreacted olefins and alcohols, and an adduct stream containing linear polyaromatic compound adducts and an olefin and unreacted linear reaction ; c) re-establishing the equilibrium (equilibrium state) in the adduct stream by partial and selective dissociation of the adducts of the linear polyaromatic compound and the olefin under conditions effective to increase the percentage of the polyaromatic compound reacted with linear alpha olefins compared to all other olefins that have reacted with polyaromatic compound in the stream, thereby obtaining a stream in a state of re-achieved equilibrium containing linear poly adducts Panchromatic compound-olefin, dissociated olefins, and unreacted and dissociated linear polyaromatic compound; d) separating the linear polyaromatic compound and olefin adducts from the dissociated olefins in an equilibrium stream to form an olefin stream containing dissociated olefins and a linear alpha olefin adduct stream containing linear polyaromatic and olefin adducts and a linear polyaromatic compound; e) dissociation of linear polyaromatic compound and olefin adducts in a linear alpha olefin adduct stream to form linear polyaromatic compounds and an alpha olefin enriched olefin product; and f) separating the alpha olefin enriched olefin product from the polyaromatic compound, where the olefin product enriched in alpha olefin is enriched in the concentration of olefins compared to the concentration of olefins in the feedstock and enriched in the concentration of linear alpha olefins in comparison with other olefins in the feedstock. 14. The method according to item 13, in which the processing mode in stage c) is implemented at a higher temperature than the processing mode in stage a). 15. The method of claim 14, wherein in step c), the adduct stream is rebalanced by heating the adduct stream at a temperature of about 280 to 310 ° C.